Apparatus for the production of formaldehyde

ABSTRACT

Apparatus and process for the production of formaldehyde by catalytic conversion of methanol wherein a reaction vessel has an outlet means and an inlet injector nozzle means at one end thereof, the injector means feeding reactants to a diffuser member, the diffuser member having at its other end an annular catalyst bed, and means in said reaction vessel for circulating reactants products passing from the catalyst bed to the outlet means and to the injector means-diffuser member for recirculation therethrough.

This is a division of application Ser. No. 359,356, filed 5/11/73, now abandoned.

This invention relates to an improved process for the production of formaldehyde by oxidation of methanol with air or other oxygen-containing gas, at temperatures within the range of 200°C to 400°C, in the presence of a catalyst containing metal oxides. More particularly, the invention relates to an apparatus adapted for use in practicing the improved process.

It is known to oxidize methanol in a reactor provided with a bundle of tube filled with a catalyst, containing a mixture of oxides, of different metals, for instance Fe, Mo, CO.

It is also known from U.S. Pat. No. 2,504,402 to let the reacting mixture of oxidizing gas and methanol pass through several catalyst layers in series, regulating the course of the reaction by means of cooling coils and injections of fresh methanol (or its mixtures with the oxidizing gas) into the interspaces between the layers.

In these processes the concentration of the formaldehyde in the gases flowing out of the reactor, must attain a minimum level of from 5 to 6% by volume. Otherwise the absorption apparatus down stream of the reactor must have such large dimensions that is very expensive.

In order to obtain a concentration of 5 to 6% formaldehyde in the effluent gases, concentrations of the same order of magnitude (6-6.5% by volume) of methanol are required in the gaseous mixture fed to the reaction zone. Such concentrations of methanol are very near the explosive range. Moreover, with such concentrations of methanol it is necessary to carefully control the temperature of the reaction to avoid excessive temperatures and too rapid reaction rates and to limit the thickness of the catalyst layers and to increase the number of layers thereof. When reactors with a plurality of catalyst layers in series are used, it is necessary to provide each layer of the catalyst with the corresponding temperature control devices (by means of external cooling and injection of quench gases) with the result that a series of complicated and costly apparatuses are required.

A further disadvantage of the prior art apparatus is that further pressure drops are required to effectively distribute the gas over the catalyst.

Still another drawback of the apparatuses of the prior art is that construction problems are encountered in installing the large diameter pipes required by the apparatus. Such pipes are subject to high thermal expansion.

As the oxidation of methanol is performed, in general, at a low pressure, further disadvantage is that a wide area is required for the apparatuses and the corresponding piping.

Therefore, an object of this invention is to provide a process for making formaldehyde by the oxidation of methanol which is devoid of the foregoing disadvantages and produces a high yield of product in a single apparatus.

Other objects will become apparent from the following descriptions with reference to the accompanying drawing illustrating in a longitudinal sectional view one embodiment of the apparatus provided by the invention.

It has now been found that the above objects may be achieved by providing an improved process for the production of formaldehyde through the oxidation of methanol with air or other oxygen-containing gas, at temperatures within the range of about 200°C and 400°C in the presence of a catalyst containing metal oxides, wherein the feed stream is admixed, outside the reaction stage, with at least one portion of the reaction product coming directly from the reaction stage, and that at least one portion of the resulting mixture is directly conveyed toward the reaction stage. In this way, a recycle of at least one portion of the raw reaction product from the outlet of the reaction stage to the inlet of the reaction stage is achieved. The cycle may be controlled in a simple and practical way through a heat exchange and it may be performed by using a compressor, an injector or any other suitable device external of the reaction stage.

By means of this recycle, it is possible to have a relatively low concentration of methanol inside the reactor itself and still produce suitable concentrations of formaldehyde leaving the reactor.

This avoids the development of excessively high temperatures on the catalyst bed and excessively high reaction rates. Consequently, devices for the control of the temperature may be reduced or eliminated. For example, cooling coils are not required if the process is an adiabatic one.

The improved process provided by the invention is more flexible, i.e., the output level can vary within a wide range, and makes it possible to make installations of high output level by using a reactor in which the number of catalyst layers can be reduced conveniently to just a single one. In this way it is possible to avoid the use of costly diathermic oils in the reaction stage to avoid stopping of the reaction.

The regulation of the temperature may be conveniently realized by cooling at least one portion of the raw product to be recycled, so that the initial contact temperature with the catalyst is between about 220°C and 300°C.

The recycle and feed streams are mixed together in such proportions as to achieve in the mixture coming into contact with the catalyst, a molar ratio of formaldehyde to methanol of between 0.3 and 5.

The space velocity of the gases impinging the catalyst is suitably between 8,000 and 20,000 h⁻ ¹ and preferably between 10,000 and 15,000 h⁻ ¹, wherein space velocity is defined as: ##EQU1##

The catalyst may be arranged in various ways inside the reactor without thereby falling outside the scope of the invention. According to a preferred embodiment of the invention, the reaction is performed in a centrifugal radial flow reactor.

According to a most preferred embodiment, the reaction is performed in an apparatus which, within one single shell has the following parts:

a centrifugal radial flow catalyst basket with a substantially cylindrical inside cavity, one end of the cavity being located immediately downstream of the terminal end of the diffuser;

an outside jacket substantially co-axial with the injector and with the basket, which jacket conveyes at least part of the gases, coming from the basket, towards the inlet of the injector;

a heat exchanger in which at least a portion of the recycling gases, coming from the basket, directly exchanges heat with another fluid.

As fluid for the heat exchanger may be used a fluid alien to the reaction, for instance water, or a fluid involved in the reaction, for example, the feed gases containing the reactants.

The just described apparatus makes it possible to obtain a low power consumption, a good distribution of the gas on the catalyst, lower pressure drops, a simplification of the problems connected with thermal expansions, a reduction of the areas and volumes engaged, as well as a simplification in the choice of the materials. In fact there may be used in a satisfactory way normal carbon steel in substitution for the costly alloy steels used in most prior art apparatuses. An example of an apparatus provided by the invention is illustrated in FIG. 1. Of course, this example is not to be taken as limiting in any way the scope of this invention.

As will be noted in said FIG. 1, the axes of the injector, the basket, the heat exchanger and the jacket coincide substantially with one single vertical rectilinear axis.

The following example is given merely for illustrative purposes and does not limit in any way the scope of the invention.

EXAMPLE 1

Referring now to FIG. 1, the feed mixture, coming from source 1 and containing 6.79% by weight CH₃ OH, 10.15% by weight O₂ and 78.84% by weight N₂ enters nozzle 3 of the reactor and draws the recycle stream 4(compressing it) along with it. The mixture enters mixing chamber 5 and then passes into diffuser 6.

From there the flow reaches chamber 7 which consists of the internal cavity of the catalytic centrifugal radial flow basket 8. This chamber is so dimensioned as to act, for all practical purposes, as a gas distributor, and having pressure drops quite negligible in comparison with the ones of the catalytic bed.

Through orifice 9, the gases reach the catalyst, which contains oxides of iron and molybdenum and react in an adiabatic way. They then pass through jacket 10 which coveyes the reacted gases directly to the heat exchanger 2 where a stream of cooling water is converted into steam.

The reacted gas divides itself at this point into two streams: the one (11) definitively discharges from the reactor and passes to the subsequent process operations (scrubbing, separation of the products, etc.); the other (4) forms, as previously indicated, the recycle. The opening 12 serves for the fast unloading of the exhausted catalyst.

Formaldehyde percentage in the gases leaving the reactor is 6.03% by weight.

Although the invention has been described with reference to particular forms of embodiment, it is understood that moditications may be introduced without thereby falling outside the spirit of the inventive idea of this invention. 

What is claimed is:
 1. An apparatus for oxidizing methanol into formaldehyde which comprisesan elongated housing enclosing a space, said housing having a first substantially cylindrical end portion, a second substantially cylindrical end portion spaced longitudinally from the first end portion, and an intermediate substantially frustoconically shaped portion connecting the two end portions together, a nozzle connected to a source of methanol and oxygen disposed longitudinally through the end of the first cylindrical portion of the housing, a tubular member coaxial with the housing and disposed in the space enclosed by the housing, said tubular member having a first substantially cylindrical end portion substantially concentric with said first end portion of the housing, a second substantially cylindrical end portion substantially concentric with the said second end portion of the housing, and a substantially frustoconical intermediate portion which is substantially concentric with the said intermediate portion of the housing, and a plurality of orifices in said second end portion of the tubular member for flow of gas therefrom, said tubular member having an open end flared outwardly disposed about the nozzle, an annular centrifugal catalyst basket disposed about the second end portion of the tubular member and spaced radially inwardly of the adjacent part of the housing, a plurality of orifices in the basket for flow of gases from the catalyst bed into space between the catalyst basket and the housing, and means extending through said housing for removing catalyst from the catalyst bed, a cooling means disposed about the first cylindrical end portion of the tubular member and means for circulating a cooling fluid through the cooling means, and an outlet for flow of gas from the space enclosed by the housing disposed adjacent to said nozzle whereby gas introduced into the apparatus through the nozzle flows through the tubular member through the catalyst into space about the tubular member and longitudinally back to the outlet and a portion of the gas flowing towards the outlet is drawn by gas emerging from the nozzle into the tubular member for recycle through the catalyst. 